WO2015037557A1 - 有機性排水の処理装置及び処理方法 - Google Patents
有機性排水の処理装置及び処理方法 Download PDFInfo
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- WO2015037557A1 WO2015037557A1 PCT/JP2014/073649 JP2014073649W WO2015037557A1 WO 2015037557 A1 WO2015037557 A1 WO 2015037557A1 JP 2014073649 W JP2014073649 W JP 2014073649W WO 2015037557 A1 WO2015037557 A1 WO 2015037557A1
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- organic wastewater
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/08—Specific process operations in the concentrate stream
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2673—Evaporation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/027—Nanofiltration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/145—Ultrafiltration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/147—Microfiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
- C02F3/1273—Submerged membrane bioreactors
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Definitions
- the present invention relates to an organic wastewater treatment apparatus and treatment method.
- the wastewater to be treated is supplied to the NF membrane module and separated into permeate and non-permeate water, the permeate is supplied to the RO membrane module, and separated into permeate and non-permeate water,
- a wastewater treatment method is known in which the non-permeate water is supplied to an evaporative concentration apparatus and concentrated.
- the present invention has been made in view of the above problems, and its object is to effectively remove organic substances, reduce the processing amount of the evaporating and concentrating device, and greatly increase the pure water recovery rate of the entire system.
- An object of the present invention is to provide an organic wastewater treatment apparatus and treatment method that can be improved.
- Embodiment 1 of the present invention includes an aerobic tank for aerobically treating organic wastewater under aerobic conditions, a microfiltration or ultrafiltration membrane separation apparatus for solid-liquid separation of treated water in the aerobic tank, A reverse osmosis membrane or nanomembrane separation device for desalting the filtrate of the microfiltration or ultrafiltration membrane separation device, and an evaporation concentration device for further concentrating the concentrated water of the reverse osmosis membrane or nanomembrane separation device.
- Organic wastewater treatment equipment for aerobically treating organic wastewater under aerobic conditions
- a microfiltration or ultrafiltration membrane separation apparatus for solid-liquid separation of treated water in the aerobic tank
- a reverse osmosis membrane or nanomembrane separation device for desalting the filtrate of the microfiltration or ultrafiltration membrane separation device
- an evaporation concentration device for further concentrating the concentrated water of the reverse osmosis membrane or nanomembrane separation device.
- Embodiment 2 of the present invention is an organic material according to Embodiment 1, further comprising an ion exchange device for ion exchange of the filtrate before the reverse osmosis membrane or nanomembrane separation device desalinates the filtrate. Wastewater treatment equipment.
- Embodiment 3 of the present invention is the organic wastewater treatment apparatus according to Embodiment 2, further comprising an alkali addition device that adds alkali to the concentrated water before the evaporative concentration device further concentrates the concentrated water. is there.
- Embodiment 4 of the present invention is the organic wastewater treatment apparatus according to Embodiment 2, further comprising a condensed water transport member that transports condensed water obtained by condensing the water evaporated from the evaporative concentration apparatus to the aerobic tank. .
- Embodiment 5 of the present invention before the evaporative concentration apparatus further concentrates the concentrated water, an alkali addition apparatus that adds alkali to the concentrated water, and condensed water obtained by condensing water evaporated from the evaporative concentration apparatus are provided. It is the processing apparatus of the organic waste_water
- Embodiment 6 of the present invention is the organic wastewater treatment apparatus according to Embodiment 1, further comprising an alkali addition device that adds alkali to the concentrated water before the evaporative concentration device further concentrates the concentrated water. is there.
- Embodiment 7 of the present invention is the organic wastewater treatment apparatus according to Embodiment 6, further comprising a condensed water transport member that transports condensed water obtained by condensing the water evaporated from the evaporative concentration apparatus to the aerobic tank. .
- Embodiment 8 of the present invention is the organic wastewater treatment apparatus according to Embodiment 1, further comprising a condensed water transport member that transports condensed water obtained by condensing the water evaporated from the evaporative concentration apparatus to the aerobic tank. is there.
- an aerobic treatment step in which an organic wastewater is aerobically treated under an aerobic condition in an aerobic tank, and treated water in the aerobic tank is solidified by a microfiltration or ultrafiltration membrane separator.
- Embodiment 10 of the present invention is the organic wastewater treatment method according to Embodiment 9, further comprising an ion exchange step of ion exchange of the filtrate by an ion exchange device before the desalting treatment step.
- Embodiment 11 of the present invention is the organic wastewater treatment method according to Embodiment 10, further comprising an alkali addition step of adding alkali to the concentrated water by an alkali addition device before the evaporation and concentration step.
- Embodiment 12 of the present invention is the organic waste water according to embodiment 10, further comprising a condensed water conveyance step of conveying condensed water obtained by condensing moisture evaporated from the evaporating and concentrating device by the condensed water conveyance member to the aerobic tank. It is a processing method.
- an alkali addition step of adding alkali to the concentrated water by an alkali addition device, and condensation condensed water evaporated from the evaporation concentration device by a condensed water transport member It is the processing method of the organic waste_water
- Embodiment 14 of the present invention is the organic wastewater treatment method according to Embodiment 9, further comprising an alkali addition step of adding alkali to the concentrated water by an alkali addition device before the evaporation and concentration step.
- Embodiment 15 of the present invention is an organic wastewater according to embodiment 14, further comprising a condensed water transporting step of transporting condensed water obtained by condensing water evaporated from the evaporating and concentrating device by a condensed water transporting member to the aerobic tank. It is a processing method.
- Embodiment 16 of the present invention is an organic wastewater according to embodiment 9, further comprising a condensed water conveyance step of conveying condensed water obtained by condensing moisture evaporated from the evaporating and concentrating device by a condensed water conveying member to the aerobic tank. It is a processing method.
- Embodiment 17 of the present invention further comprises a chemical washing step for washing the filtration membrane of the membrane separation unit of the microfiltration or ultrafiltration membrane separation device in a state where the solid-liquid separation step is stopped, the chemical washing step A chemical solution injection step of injecting a chemical solution into the membrane separation unit of the microfiltration or ultrafiltration membrane separation device to wash the filtration membrane, and a state in which the chemical solution is injected into the membrane separation unit,
- a water washing step of injecting into the membrane separation unit of the ultrafiltration membrane separator and washing the filtration membrane with water, and the microfiltration or ultrafiltration membrane separator from the membrane separation unit through the aeration pipe with water after washing Discharged into the membrane separation tank Process and a method of treating organic waste water according to technical solution 9 comprising a.
- Embodiment 18 of the present invention is the organic wastewater treatment method according to Embodiment 17, wherein the chemical solution is a hypochlorite chemical solution.
- Embodiment 19 of the present invention is the organic wastewater treatment method according to embodiment 18, wherein the chemical washing step is performed once again, and in the second chemical washing step, the chemical solution is an acidic chemical solution.
- organic substances can be effectively removed, the processing amount of the evaporative concentration apparatus is reduced, and the pure water recovery rate of the entire system is greatly improved.
- divalent ion components in the filtrate can be removed, and scaling can be prevented from occurring in the reverse osmosis membrane or nano membrane separation device and the evaporation concentration device.
- the alkali concentrator and the process can prevent the evaporative concentrator from being corroded by chlorine.
- the condensed water transport member and the process the heat generated from the evaporative concentration device is supplied to the aerobic tank, the activated sludge in the aerobic tank is activated, and the processing efficiency and the filtration efficiency are improved.
- Reverse osmosis membrane or nano membrane separation device avoids high concentrations of hypochlorite, acid, active surfactant, etc. from being mixed in the filtrate filtered by the filtration membrane separation device by the water washing process and discharge process Can be adversely affected.
- coke dry fire extinguishing equipment Coke Dry Quenching / CDQ
- the coke wastewater contains a lot of refractory organic substances such as humin and toxic substances such as cyan and phenol, so that the biological treatment tank becomes unstable, which is one of the reasons why the RO recovery rate cannot be improved.
- the biological reaction tank is heated by the high-temperature condensed water generated from the evaporation concentrator, stable biological treatment is possible, and the RO / NF recovery rate can be improved and the subsequent evaporator concentrator can be downsized. .
- FIG. 1 is a schematic diagram of an organic wastewater treatment apparatus of the present invention.
- FIG. 2 is a schematic diagram of the aerobic tank and the microfiltration or ultrafiltration membrane separation device of the present invention, and illustrates the hypochlorite chemical solution injection step.
- FIG. 3 is a schematic diagram of the aerobic tank and the microfiltration or ultrafiltration membrane separation device portion of the present invention, illustrating the stationary process.
- FIG. 4 is a schematic view of the aerobic tank and the microfiltration or ultrafiltration membrane separation apparatus part of the present invention, illustrating the air diffusion step.
- FIG. 5 is a schematic view of the aerobic tank and the microfiltration or ultrafiltration membrane separation device of the present invention, illustrating the water washing step.
- FIG. 1 is a schematic diagram of an organic wastewater treatment apparatus of the present invention.
- FIG. 2 is a schematic diagram of the aerobic tank and the microfiltration or ultrafiltration membrane separation device of the present invention, and illustrates the hypochlorite chemical solution injection step.
- FIG. 3 is a schematic diagram of the aerobic tank and the microfiltration or
- FIG. 6 is a schematic diagram of the aerobic tank and the microfiltration or ultrafiltration membrane separation apparatus portion of the present invention, illustrating the discharge process.
- FIG. 7 is a schematic diagram of the aerobic tank and the microfiltration or ultrafiltration membrane separation device portion of the present invention, illustrating an acidic chemical solution injection step.
- the organic wastewater treatment apparatus mainly includes an aerobic tank 4, a microfiltration or ultrafiltration membrane separation device 5, a water softener 6 serving as an ion exchange device, and a reverse osmosis membrane or A nanomembrane separation device 7, an alkali addition device 8, and an evaporation concentration device 9 are provided.
- Raw water used as organic wastewater is first introduced into the aerobic tank 4.
- the raw water is subjected to aerobic treatment under aerobic conditions. That is, the aeration tube 41 is provided in the aerobic tank 4, and after introducing air into the aeration tube 41 by the floor B1, the air is diffused in the aeration tube 41, and the aerobic microorganisms in the aerobic tank 4 Decompose organic matter.
- the microfiltration or ultrafiltration membrane separation device 5 performs solid-liquid separation of the treated water treated in the aerobic tank 4.
- the microfiltration or ultrafiltration membrane separation device 5 includes a membrane separation tank 51, a diffuser tube 52, and a membrane separation unit 53.
- the membrane separation unit 53 is provided in the membrane separation tank 51 using a microfiltration membrane (MF membrane) or an ultrafiltration membrane (UF membrane).
- the air diffuser 52 is provided below the membrane separation unit 53.
- the treated water treated in the aerobic tank 4 is introduced into the membrane separation tank 51.
- the treated water is separated into solid and liquid by the membrane separation unit 53.
- air is introduced into the diffuser pipe 52 by the floor B1, diffused in the membrane separation tank 51, and the filtration membrane of the membrane separation unit 53 is vibrated by the flow of the aeration, thereby preventing clogging of the pores of the filtration membrane.
- the microfiltration membrane (MF membrane) or ultrafiltration membrane (UF membrane) of the membrane separation unit 53 may be any of a flat membrane, a tubular membrane, a hollow fiber membrane, and the like.
- the filtrate after solid-liquid separation passes through the water softener 6, and the filtrate is ion-exchanged with the water softener 6 to remove divalent ion components such as Ca ions and Mg ions in the filtrate, and reverse osmosis membrane or nano membrane separation. Scaling is prevented from occurring in the apparatus and the evaporative concentration apparatus.
- the reverse osmosis membrane or nanomembrane separation device 7 desalinates the filtrate, filtrate water tank 71, first-stage reverse osmosis membrane or nanomembrane separation module 72, and second-stage reverse osmosis membrane or nanomembrane.
- a separation module 73 is provided.
- the reverse osmosis membrane or nanomembrane separation device 7 may be one-stage processing or two-stage processing.
- the reverse osmosis membrane or the reverse osmosis membrane (RO membrane) or nanomembrane (NF membrane) of the nanomembrane separation device 7 may be any one of a flat membrane, a tubular membrane, a hollow fiber membrane, a spiral membrane and the like.
- the ion-exchanged filtrate is introduced into the filtrate water tank 71, it is supplied to the first-stage reverse osmosis membrane or nanomembrane separation module 72 and filtered through the first-stage reverse osmosis membrane or nanomembrane separation module 72.
- the first-stage treated water is introduced into the second-stage reverse osmosis membrane or nanomembrane separation module 73, and the first-stage concentrated water discharged from the first-stage reverse osmosis membrane or nanomembrane separation module 72 is A part is introduced into the concentrated raw water tank 10, and the other part is mixed into the filtrate and introduced again into the first-stage reverse osmosis membrane or nanomembrane separation module 72.
- the second-stage treated water filtered by the second-stage reverse osmosis membrane or nano-membrane separation module 73 is recovered and used, and the second-stage concentration from the second-stage reverse osmosis membrane or nano-membrane separation module 73 is recovered.
- a part of the water is returned to the filtrate water tank 71, and the other part is mixed into the first-stage treated water and introduced again into the second-stage reverse osmosis membrane or nano-membrane separation module 73.
- the first stage concentrated water in the concentrated raw water tank 10 is introduced into the evaporative concentration apparatus 9.
- the first stage concentrated water is heated, evaporated under reduced pressure, and further concentrated. Further, the concentrated water is introduced into the concentrated water tank 11 and discarded as industrial waste.
- Condensed water obtained by condensing water evaporated by the evaporating and concentrating device 9 is conveyed to the aerobic tank 4 by the conveying pipe 12 serving as a condensed water conveying member. Therefore, the heat generated from the evaporating and concentrating device 9 is also supplied to the aerobic tank 4 and the activated sludge in the aerobic tank 4 is activated to improve the processing efficiency and the filtration efficiency.
- a chemical washing process for washing the filtration membrane of the microfiltration or ultrafiltration membrane separation apparatus of the present invention will be described with reference to FIGS.
- the chemical washing step is to wash the filtration membrane of the membrane separation unit 53 in a state where the solid-liquid separation with respect to the treated water of the microfiltration or ultrafiltration membrane separation device 5 is stopped.
- a process, a stationary process, an air diffusion process, a water washing process, a discharge process, an acidic chemical solution injection process, a stationary process, an air diffusion process, a water washing process, and a discharge process are performed.
- the hypochlorite chemical injection step the hypochlorite chemical is injected into the membrane separation unit 53 of the microfiltration or ultrafiltration membrane separation device 5 to wash the filtration membrane. That is, as shown in FIG. 2, the pump P1 is operated, the filtrate filtered by the membrane separation unit 53 and stored in the water storage tank 12 is introduced into the membrane separation unit 53, and the pump P2 is operated to perform hypochlorite.
- the hypochlorite chemical stored in the chemical tank 13 is introduced into the membrane separation unit 53, and the filtrate and the hypochlorite chemical are mixed together at location A and introduced together into the membrane separation unit 53. 53 filtration membranes are washed.
- the hypochlorite chemical may be made by adding NaClO, Ca (ClO) 2 , ClKO or the like to industrial water.
- the operation of the pump P3 is stopped, and the introduction of the acidic chemical solution stored in the acidic chemical solution tank 14 to the membrane separation unit 53 is stopped.
- the operation of the floor B1 is stopped, and the introduction of the air into the diffuser pipe 41 in the treatment tank 4 and the diffuser pipe 54 and the diffuser pipe 52 in the membrane separation tank 51 is stopped. Therefore, the air diffuser of the air diffuser 41, the air diffuser 54, and the air diffuser 52 is stopped.
- the operation of the pump P4 is stopped, and the derivation of the filtrate from the membrane separation unit 53 is stopped.
- the microfiltration or ultrafiltration membrane separation device 5 enters a state where the aeration operation is stopped in a state where the hypochlorite chemical solution is injected into the membrane separation unit 53. That is, as shown in FIG. 3, the operations of the pump P1, the pump P2, and the pump P3 are stopped, and the introduction of the filtrate, hypochlorite chemical, and acidic chemical into the membrane separation unit 53 is stopped. At the same time, the operation of the floor B1 is stopped, and the introduction of the air into the diffuser pipe 41 of the treatment tank 4 and the diffuser pipe 54 and the diffuser pipe 52 in the membrane separation tank 51 is stopped. Therefore, the air diffuser of the air diffuser 41, the air diffuser 54, and the air diffuser 52 is stopped. At the same time, the operation of the pump P4 is stopped, and the derivation of the filtrate from the membrane separation unit 53 is stopped.
- air diffusion step air is diffused into the microfiltration or ultrafiltration membrane separation device 5. That is, as shown in FIG. 4, the floor B ⁇ b> 1 is operated, and air is introduced into the diffuser pipe 41 in the treatment tank 4 and the diffuser pipe 54 and the diffuser pipe 52 in the membrane separation tank 51. Therefore, the diffuser 41, the diffuser 54, and the diffuser 52 are diffused.
- the operations of the pump P1, the pump P2, and the pump P3 are stopped, and the introduction of the filtrate, hypochlorite chemical solution, and acidic chemical solution into the membrane separation unit 53 is stopped.
- the operation of the pump P4 is stopped, and the derivation of the filtrate from the membrane separation unit 53 is stopped.
- water is injected into the membrane separation unit 53 of the microfiltration or ultrafiltration membrane separation device 5 to wash the filtration membrane. That is, as shown in FIG. 5, the pump P1 is operated, the filtrate filtered by the membrane separation unit 53 and stored in the water storage tank 12 is introduced into the membrane separation unit 53, and the filtration membrane is washed with water.
- the floor B1 is operated, and air is introduced into the diffuser pipe 41 in the treatment tank 4 and the diffuser pipe 54 and the diffuser pipe 52 in the membrane separation tank 51, respectively. Therefore, the diffuser 41, the diffuser 54, and the diffuser 52 are diffused.
- the operation of the pump P2 and the pump P3 is stopped, and the introduction of the hypochlorite chemical solution and the acidic chemical solution into the membrane separation unit 53 is stopped.
- the operation of the pump P4 is stopped, and the derivation of the filtrate from the membrane separation unit 53 is stopped.
- the water after washing returns to the aeration pipe 52 and is discharged to the membrane separation tank 51 of the microfiltration or ultrafiltration membrane separation device 5. That is, as shown in FIG. 6, the pump P ⁇ b> 4 is operated and the water after washing is led out from the membrane separation unit 53.
- the floor B1 is operated, and air is introduced into the diffuser pipe 41 in the treatment tank 4 and the diffuser pipe 54 and the diffuser pipe 52 in the membrane separation tank 51, respectively. Therefore, the diffuser 41, the diffuser 54, and the diffuser 52 are diffused.
- the water and air after the water washing are mixed at the point C, and both are introduced into the diffuser tube 52, and thus the water after the water washing enters the membrane separation tank 51.
- the operations of the pump P1, the pump P2, and the pump P3 are stopped, and the introduction of the filtrate, hypochlorite chemical solution, and acidic chemical solution into the membrane separation unit 53 is stopped.
- the acidic chemical solution injection step the acidic chemical solution is injected into the membrane separation unit 53 of the microfiltration or ultrafiltration membrane separation device 5 to wash the filtration membrane.
- the pump P1 is operated, the filtrate filtered by the membrane separation unit 53 and stored in the water storage tank 12 is introduced into the membrane separation unit 53, and the pump P3 is operated and stored in the acidic chemical liquid tank 14.
- the acidic chemical solution is introduced into the membrane separation unit 53, the filtrate and the acidic chemical solution are mixed at the B location, and introduced together into the membrane separation unit 53, and the filtration membrane of the membrane separation unit 53 is washed.
- the acidic chemical solution may be made by adding H 2 SO 4 or the like to industrial water.
- the operation of the pump P2 is stopped and the introduction of the hypochlorite chemical stored in the hypochlorite chemical tank 13 to the membrane separation unit 53 is stopped.
- the operation of the floor B1 is stopped, and the introduction of the air into the diffuser pipe 41 in the treatment tank 4 and the diffuser pipe 54 and the diffuser pipe 52 in the membrane separation tank 51 is stopped. Therefore, the air diffuser of the air diffuser 41, the air diffuser 54, and the air diffuser 52 is stopped.
- the operation of the pump P4 is stopped, and the derivation of the filtrate from the membrane separation unit 53 is stopped. Thereafter, the stationary step, the air diffusion step, the water washing step, and the discharging step are performed once more.
- the organic wastewater treatment apparatus further includes an oil / water separation tank, a flow rate adjustment tank, and a pressurized flotation device.
- the raw water is first introduced into the oil / water separation tank. Oil is separated from raw water in an oil-water separation tank. And the raw
- a flow rate adjustment tank controls the flow rate introduced into the pressurized levitation device of the raw water.
- the pressurized levitation device floats and removes floating substances containing SiO 2 and Ca in the raw water.
- the pressure levitation device includes a reaction tank, a pressure levitation tank, and a neutralization tank.
- raw water is introduced into a reaction tank, and polyaluminum chloride (PAC) and polyacrylamide (PAM) as flocculants are placed in order in the two reaction tanks, and stirred with a stirrer to obtain polyaluminum chloride (PAC), Polyacrylamide (PAM) is sufficiently solubilized in the raw water, and suspended substances aggregate.
- PAC polyaluminum chloride
- PAM polyacrylamide
- air is injected into the raw water by an air injecting device, a large amount of fine bubbles are generated, and the aggregated suspended solids in the raw water are captured by the fine bubbles. Lift using buoyancy. After the suspended matter floats up to the surface of the raw water, the suspended matter is removed from the surface by a scraping device.
- SiO 2 has a gel shape and a negative charge.
- PAC polyaluminum chloride
- SiO 2 aggregates and floats and is removed from the raw water as described above.
- Ca it elutes in raw
- Na 2 CO 3 is previously placed in the flow rate adjusting tank, Ca is not dissolved in the raw water, and is agglomerated by the aggregating agent, floated, and removed from the raw water as described above.
- Raw water from which suspended solids have been removed is introduced into the neutralization tank.
- H 2 SO 4 is put into the neutralization tank to neutralize the raw water.
- the raw water whose pH value is adjusted is put into the aerobic tank 4, and the aerobic treatment step, the solid-liquid separation step, the ion exchange step, the desalting treatment step, the alkali addition step, the evaporation concentration step, and the condensed water conveyance are sequentially performed. Perform the process.
- the raw water amount for treatment is 8 to 10 m 3 / d during operation and 16 m 3 / d at design time.
- the amount of raw water for treatment is 1 m 3 / d
- the water area load is 24 m 3 / m 2 / d
- the residence time is 2.8 h.
- the injection rate of polyaluminum chloride (PAC) is 500 mg PAC pure fraction / L
- the polyacrylamide (PAM) injection rate is 3 mg PAM pure fraction / L.
- the pH value of the reaction tank is 8.5
- the pH value of the neutralization tank is 7.5.
- the volumetric load of biochemical oxygen demand is 0.045 kg BOD / m 3 / d.
- the biochemical oxygen demand (BOD) sludge load is 0.015 kg BOD / kg MLSS / d.
- the flux of the filtration membrane is 0.18 m 3 / m 2 / d.
- the amount of raw water for treatment is 1 m 3 / h
- the amount of treated water is 0.8 m 3 / h
- the recovery rate is 80% or more.
- the reverse osmosis membrane or nanomembrane separation module 72 in the first stage of the reverse osmosis membrane or nanomembrane separation device 7 is a contamination-resistant low-pressure spiral RO membrane element (manufactured by Nitto Denko: LFC3-LD-4040).
- the flux is 0.33 m 3 / m 2 / d.
- the first-stage reverse osmosis membrane or nanomembrane separation module 72 is 80%
- the second-stage reverse osmosis membrane or nanomembrane separation module 73 is 88%.
- the amount of raw water for the treatment is 1.6 to 3.2 m 3 / d, which can be concentrated 8 to 16 times, and the concentrated water that has come out is 0.2 m 3 / d.
- the evaporating and concentrating device 9 is a vacuum evaporating steam heating type (treatment water amount: 3.2 m 3 / d device structure: open frame type).
- the organic wastewater treatment apparatus includes the aerobic tank 4, the microfiltration or ultrafiltration membrane separation device 5, the water softener 6 serving as an ion exchange device, the reverse osmosis membrane or the nano-scale.
- a membrane separation device 7, an alkali addition device 8, an evaporation concentration device 9, and a condensed water transport member are provided.
- the present invention is not limited to this, and the organic wastewater treatment device is an aerobic tank 4, a microfiltration or ultrafiltration membrane separation device 5, a reverse osmosis membrane or nanomembrane separation device 7, and evaporation concentration.
- drain may also contain any one or more among these apparatuses, the water softener 6, the alkali addition apparatus 8, and a condensed water conveyance member.
- the chemical washing process includes the hypochlorite chemical injection process, the stationary process, the air diffusion process, the water washing process, the discharge process, the acidic chemical liquid injection process, the static process, and the air diffusion process.
- a process, a water washing process, and a discharge process are provided.
- the present invention is not limited to this, and the chemical washing process may include only a hypochlorite chemical liquid injection process, a stationary process, an air diffusion process, a water washing process, and a discharge process.
- organic substances can be effectively removed, the processing amount of the evaporative concentration apparatus is reduced, and the pure water recovery rate of the entire system is greatly improved.
- divalent ion components in the filtrate can be removed, and scaling can be prevented from occurring in the reverse osmosis membrane or nano membrane separation device and the evaporation concentration device.
- the alkali concentrator and the process can prevent the evaporative concentrator from being corroded by chlorine.
- the condensed water transport member and the process the heat generated from the evaporative concentration device is supplied to the aerobic tank, the activated sludge in the aerobic tank is activated, and the processing efficiency and the filtration efficiency are improved.
- Reverse osmosis membrane or nano membrane separation device avoids high concentrations of hypochlorite, acid, active surfactant, etc. from being mixed in the filtrate filtered by the filtration membrane separation device by the water washing process and discharge process Can be adversely affected. Furthermore, in the present invention, the biological reaction tank is heated by the high-temperature condensate generated from the evaporation concentrator, so that stable biological treatment is possible, and the RO / NF recovery rate can be improved and the subsequent evaporator concentrator can be downsized. It becomes.
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Abstract
Description
イオン交換装置及び工程によって、ろ液内の二価イオン成分を除去し、逆浸透膜又はナノ膜分離装置及び蒸発濃縮装置内でスケーリングが発生することを防止できる。
アルカリ添加装置及び工程によって、蒸発濃縮器が塩素腐食することを防止できる。
凝縮水搬送部材及び工程によって、蒸発濃縮装置から出た熱を好気槽に供給し、好気槽内の活性汚泥を活性化させ、処理効率、濾過効率を向上させる。
水洗工程及び排出工程によって、次亜塩素酸塩、酸、活性界面剤等のものが高濃度でろ過膜分離装置で濾過したろ液に混入することを回避し、逆浸透膜又はナノ膜分離装置に悪影響を与えることを防止できる。
特にコークス産業では、コークス乾式消火設備(Coke Dry Quenching/CDQ)の導入促進に伴い、排水処理水質の高度化および排水量ゼロ化の技術が求められている。
コークス排水中には、フミン等の難分解性有機物やシアン・フェノールといった毒性物質が多く含まれるため生物処理槽が不安定となり、RO回収率を向上できない原因の一つとなっていた。
図1の示すように、有機性排水の処理装置は、主に、好気槽4と、精密ろ過又は限外ろ過膜分離装置5と、イオン交換装置とする軟水器6と、逆浸透膜又はナノ膜分離装置7と、アルカリ添加装置8と、蒸発濃縮装置9とを備える。
イオン交換したろ液は、ろ液水槽71に導入された後に、1段目の逆浸透膜又はナノ膜分離モジュール72に供給され、1段目の逆浸透膜又はナノ膜分離モジュール72で濾過した1段目の処理水は、2段目の逆浸透膜又はナノ膜分離モジュール73に導入され、1段目の逆浸透膜又はナノ膜分離モジュール72から出た1段目の濃縮水は、その一部が濃縮原水水槽10に導入され、他部がろ液に混入してあらためて1段目の逆浸透膜又はナノ膜分離モジュール72に導入される。2段目の逆浸透膜又はナノ膜分離モジュール73で濾過した2段目の処理水を回収して利用し、2段目の逆浸透膜又はナノ膜分離モジュール73から出た2段目の濃縮水は、その一部がろ液水槽71に戻し、他部が1段目の処理水に混入してあらためて2段目の逆浸透膜又はナノ膜分離モジュール73に導入される。
濃縮原水水槽10内の1段目の濃縮水は、蒸発濃縮装置9に導入される。蒸発濃縮装置9では、1段目の濃縮水を加熱し、減圧の状態でそれを蒸発し、さらに濃縮する。さらに濃縮した濃縮水は、濃縮水槽11に導入され、産業廃棄物として廃棄する。
凝縮水搬送部材とする搬送管12により、蒸発濃縮装置9で蒸発した水分を凝縮した凝縮水を好気槽4へ搬送する。よって、蒸発濃縮装置9から出た熱もそれに連れて好気槽4に供給され、好気槽4内の活性汚泥を活性化させ、処理効率、濾過効率を向上させる。
薬洗工程は、精密ろ過又は限外ろ過膜分離装置5の処理水に対する固液分離が停止する状態で、膜分離ユニット53のろ過膜を洗浄するものであり、順に次亜塩素酸塩薬液注入工程、静置工程、空散気工程、水洗工程、排出工程、酸性薬液注入工程、静置工程、空散気工程、水洗工程、排出工程を行う。
つまり、図2の示すように、ポンプP1が運転し、膜分離ユニット53で濾過し貯水槽12に貯蔵したろ液を膜分離ユニット53へ導入し、ポンプP2が運転し、次亜塩素酸塩薬液槽13に貯蔵した次亜塩素酸塩薬液を膜分離ユニット53へ導入し、ろ液と次亜塩素酸塩薬液がA箇所で混合して一緒に膜分離ユニット53に導入され、膜分離ユニット53の濾過膜を洗浄する。次亜塩素酸塩薬液は、工業用水にNaClO、Ca(ClO)2やClKO等を添加することで作られてもよい。
同時に、ポンプP3の運転が停止し、酸性薬液槽14に貯蔵した酸性薬液の膜分離ユニット53への導入が停止する。
同時に、フロアーB1の運転が停止し、空気の処理槽4内の散気管41、膜分離槽51内の散気管54や散気管52への導入が停止する。よって、散気管41、散気管54、散気管52の散気が停止する。
同時に、ポンプP4の運転が停止し、ろ液の膜分離ユニット53からの導出が停止する。
つまり、図3の示すように、ポンプP1、ポンプP2及びポンプP3の運転が停止し、ろ液、次亜塩素酸塩薬液及び酸性薬液の膜分離ユニット53への導入が停止する。同時に、フロアーB1の運転が停止し、空気の処理槽4の散気管41、膜分離槽51内の散気管54や散気管52への導入が停止する。よって、散気管41、散気管54、散気管52の散気が停止する。同時に、ポンプP4の運転が停止し、ろ液の膜分離ユニット53からの導出が停止する。
つまり、図4の示すように、フロアーB1が運転し、空気が処理槽4内の散気管41、膜分離槽51内の散気管54や散気管52へそれぞれ導入される。よって、散気管41、散気管54及び散気管52が散気する。
同時に、ポンプP1、ポンプP2及びポンプP3の運転が停止し、ろ液、次亜塩素酸塩薬液及び酸性薬液の膜分離ユニット53への導入が停止する。同時に、ポンプP4の運転が停止し、ろ液の膜分離ユニット53からの導出が停止する。
つまり、図5の示すように、ポンプP1が運転し、膜分離ユニット53で濾過し貯水槽12に貯蔵したろ液が膜分離ユニット53に導入され、濾過膜を水洗する。フロアーB1が運転し、空気が処理槽4内の散気管41、膜分離槽51内の散気管54や散気管52へそれぞれ導入される。よって、散気管41、散気管54及び散気管52が散気する。
同時に、ポンプP2及びポンプP3の運転が停止し、次亜塩素酸塩薬液及び酸性薬液の膜分離ユニット53への導入が停止する。
同時に、ポンプP4の運転が停止し、ろ液の膜分離ユニット53からの導出が停止する。
つまり、図6の示すように、ポンプP4が運転し、水洗後の水が膜分離ユニット53から導出される。フロアーB1が運転し、空気が処理槽4内の散気管41、膜分離槽51内の散気管54や散気管52へそれぞれ導入される。よって、散気管41、散気管54及び散気管52が散気する。また、水洗後の水と空気がC箇所で混合し、共に散気管52に導入され、よって、水洗後の水が膜分離槽51に入る。
同時に、ポンプP1、ポンプP2及びポンプP3の運転が停止し、ろ液、次亜塩素酸塩薬液及び酸性薬液の膜分離ユニット53への導入が停止する。
図7の示すように、ポンプP1が運転し、膜分離ユニット53で濾過し貯水槽12に貯蔵したろ液を膜分離ユニット53へ導入し、ポンプP3が運転し、酸性薬液槽14に貯蔵した酸性薬液を膜分離ユニット53へ導入し、ろ液と酸性薬液がB箇所で混合して共に膜分離ユニット53に導入され、膜分離ユニット53の濾過膜を洗浄する。酸性薬液は、工業用水にH2SO4等を添加することで作られても良い。
同時に、ポンプP2の運転が停止し、次亜塩素酸塩薬液槽13に貯蔵した次亜塩素酸塩薬液の膜分離ユニット53への導入が停止する。
同時に、フロアーB1の運転が停止し、空気の処理槽4内の散気管41、膜分離槽51内の散気管54や散気管52への導入が停止する。よって、散気管41、散気管54、散気管52の散気が停止する。
同時に、ポンプP4の運転が停止し、ろ液の膜分離ユニット53からの導出が停止する。
その後、前記の静置工程、空散気工程、水洗工程及び排出工程をもう一回に行う。
有機性排水の処理装置が油水分離槽、流量調整槽及び加圧浮上装置をさらに含むのが好ましい。
そして、油を分離した原水を流量調整槽に導入する。流量調整槽により、原水の加圧浮上装置へ導入する流量を制御する。
加圧浮上装置は、原水内のSiO2及びCaを含む浮遊物質を浮上させて除去する。加圧浮上装置は、反応槽、加圧浮上槽及び中和槽を含む。
そして、加圧浮上槽において、空気注入装置により、空気を原水に注入し、微細な気泡を大量に発生させ、微細な気泡により原水中の凝集した浮遊物質を捕えさせた後、微細な気泡の浮力を利用して浮上させる。浮遊物質が原水の水面に浮上した後、掻き取り装置により、浮遊物質を水面から取り除く。
Caについては、反応槽とするコンクリート水槽から原水に溶出する。Caを除去するために、予めに流量調整槽にNa2CO3を入れ、Caを原水に溶化させず、そして前記の凝集剤により凝集させ、浮上させ、前記のように原水から取り除かれる。
浮遊物質を取り除いた原水が中和槽に導入される。中和槽にH2SO4を入れ、原水を中和させる。
その後、pH値が調整された原水を好気槽4に入れ、順に前記の好気処理工程、固液分離工程、イオン交換工程、脱塩処理工程、アルカリ添加工程、蒸発濃縮工程及び凝縮水搬送工程を行う。
逆浸透膜又はナノ膜分離装置7の2段目の逆浸透膜又はナノ膜分離モジュール73は、超低圧RO膜エレメント(日東電工製:ESPA2-4040)であり、濾過膜の膜面積が7.9m2/本×6本=47m2であり、フラックスが0.41m3/m2/dである。
回収率については、1段目の逆浸透膜又はナノ膜分離モジュール72が80%であり、2段目の逆浸透膜又はナノ膜分離モジュール73が88%である。
また、有機性排水の処理装置がこれらの装置と、軟水器6、アルカリ添加装置8及び凝縮水搬送部材うちのいずれか一つ以上を含んでも良い。
さらに、本発明では蒸発濃縮装置から発生する高温の凝縮水により生物反応槽を加熱するため、安定した生物処理が可能となり、RO/NF回収率の向上および後段の蒸発濃縮装置の小型化が可能となる。
5 精密ろ過又は限外ろ過膜分離装置
6 軟水器
7 逆浸透膜又はナノ膜分離装置
8 アルカリ添加装置
9 蒸発濃縮装置
10 濃縮原水水槽
11 濃縮水槽
12 搬送管
Claims (19)
- 有機性排水を好気性条件化で好気処理する好気槽と、
前記好気槽における処理水を固液分離する精密ろ過又は限外ろ過膜分離装置と、
前記精密ろ過又は限外ろ過膜分離装置のろ液を脱塩処理する逆浸透膜又はナノ膜分離装置と、
前記逆浸透膜又はナノ膜分離装置の濃縮水をさらに濃縮する蒸発濃縮装置と、を備えることを特徴とする有機性排水の処理装置。 - 前記逆浸透膜又はナノ膜分離装置が前記ろ液を脱塩処理する前に、前記ろ液をイオン交換するイオン交換装置を更に備えることを特徴とする請求項1に記載の有機性排水の処理装置。
- 前記蒸発濃縮装置が前記濃縮水を更に濃縮する前に、前記濃縮水にアルカリを添加するアルカリ添加装置を更に備えることを特徴とする請求項2に記載の有機性排水の処理装置。
- 前記蒸発濃縮装置より蒸発した水分を凝縮した凝縮水を前記好気槽へ搬送する凝縮水搬送部材を更に備えることを特徴とする請求項2に記載の有機性排水の処理装置。
- 前記蒸発濃縮装置が前記濃縮水を更に濃縮する前に、前記濃縮水にアルカリを添加するアルカリ添加装置と、前記蒸発濃縮装置より蒸発した水分を凝縮した凝縮水を前記好気槽へ搬送する凝縮水搬送部材と、を更に備えることを特徴とする請求項2に記載の有機性排水の処理装置。
- 前記蒸発濃縮装置が前記濃縮水を更に濃縮する前に、前記濃縮水にアルカリを添加するアルカリ添加装置を更に備えることを特徴とする請求項1に記載の有機性排水の処理装置。
- 前記蒸発濃縮装置より蒸発した水分を凝縮した凝縮水を前記好気槽へ搬送する凝縮水搬送部材を更に備えることを特徴とする請求項6に記載の有機性排水の処理装置。
- 前記蒸発濃縮装置より蒸発した水分を凝縮した凝縮水を前記好気槽へ搬送する凝縮水搬送部材とを更に備えることを特徴とする請求項1に記載の有機性排水の処理装置。
- 好気槽によって有機性排水を好気性条件化で好気処理する好気処理工程と、
精密ろ過又は限外ろ過膜分離装置によって前記好気槽における処理水を固液分離する固液分離工程と、
逆浸透膜又はナノ膜分離装置によって前記精密ろ過又は限外ろ過膜分離装置のろ液を脱塩処理する脱塩処理工程と、
蒸発濃縮装置によって前記逆浸透膜又はナノ膜分離装置の濃縮液をさらに濃縮する蒸発濃縮工程と、を備えることを特徴とする有機性排水の処理方法。 - 前記脱塩処理工程の前に、イオン交換装置によって前記ろ液をイオン交換するイオン交換工程を更に備えることを特徴とする請求項9に記載の有機性排水の処理方法。
- 前記蒸発濃縮工程の前に、アルカリ添加装置によって前記濃縮水にアルカリを添加するアルカリ添加工程を更に備えることを特徴とする請求項10に記載の有機性排水の処理方法。
- 凝縮水搬送部材によって前記蒸発濃縮装置より蒸発した水分を凝縮した凝縮水を前記好気槽へ搬送する凝縮水搬送工程を更に備えることを特徴とする請求項10に記載の有機性排水の処理方法。
- 前記蒸発濃縮工程の前に、アルカリ添加装置によって前記濃縮水にアルカリを添加するアルカリ添加工程と、凝縮水搬送部材によって前記蒸発濃縮装置より蒸発した水分を凝縮した凝縮水を前記好気槽へ搬送する凝縮水搬送工程と、を更に備えることを特徴とする請求項10に記載の有機性排水の処理方法。
- 前記蒸発濃縮工程の前に、アルカリ添加装置によって前記濃縮水にアルカリを添加するアルカリ添加工程を更に備えることを特徴とする請求項9に記載の有機性排水の処理方法。
- 凝縮水搬送部材によって前記蒸発濃縮装置より蒸発した水分を凝縮した凝縮水を前記好気槽へ搬送する凝縮水搬送工程を更に備えることを特徴とする請求項14に記載の有機性排水の処理方法。
- 凝縮水搬送部材によって前記蒸発濃縮装置より蒸発した水分を凝縮した凝縮水を前記好気槽へ搬送する凝縮水搬送工程を更に備えることを特徴とする請求項9に記載の有機性排水の処理方法。
- 前記固液分離工程が停止する状態で、前記精密ろ過又は限外ろ過膜分離装置の膜分離ユニットのろ過膜を洗浄する薬洗工程を更に備え、該薬洗工程は、薬液を前記精密ろ過又は限外ろ過膜分離装置の膜分離ユニットに注入して前記ろ過膜を洗浄する薬液注入工程と、
前記膜分離ユニットに薬液を注入した状況で、前記精密ろ過又は限外ろ過膜分離装置を散気パイプによる散気が停止する状態となる静置工程と、
前記精密ろ過又は限外ろ過膜分離装置に前記散気を行う空散気工程と、
水を前記精密ろ過又は限外ろ過膜分離装置の膜分離ユニットに注入して前記ろ過膜を水洗する水洗工程と、
水洗後の水を前記膜分離ユニットから前記散気パイプを通して前記精密ろ過又は限外ろ過膜分離装置の膜分離槽に排出する排出工程と、を備えることを特徴とする請求項9に記載の有機性排水の処理方法。 - 前記薬液は、次亜塩素酸塩薬液であることを特徴とする請求項17に記載の有機性排水の処理方法。
- 前記薬洗工程をもう一回行い、第二回の薬洗工程において、前記薬液は、酸性薬液であることを特徴とする請求項18に記載の有機性排水の処理方法。
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